Gas-liquid mixer and application thereof in cumene oxidation

Abstract

The invention relates to the technical field of chemical equipment, and discloses a gas-liquid mixer and application of the gas-liquid mixer in cumene oxidation.The gas-liquid mixer comprises a mixer shell provided with a first under-pressure inflation area and a second under-pressure inflation area, an injection pipe is arranged in the first under-pressure inflation area, a porous material membrane pipe is arranged in the second under-pressure inflation area, and the first under-pressure inflation area and the second under-pressure inflation area are communicated through the injection pipe. The injection pipe and the porous material membrane pipe are coaxially connected to form a continuous internal flow channel for liquid to flow through; the injection pipe comprises a liquid inlet section, a throttling section, a gas inlet section and a gas-liquid two-phase development section which are sequentially arranged in the flowing direction of liquid, the flow channel sectional area of the liquid inlet section and the flow channel sectional area of the gas inlet section are equal and larger than the flow channel sectional area of the throttling section, and the gas inlet section and the porous material membrane pipe are used for introducing gas into an internal flow channel; the gas-liquid mixer provided by the invention realizes efficient mixing of gas and liquid phases under the conditions of high flux and high gas-liquid ratio, and effectively overcomes the defect that a large number of micro-nano bubbles cannot be formed under the conditions of high flux and high gas-liquid ratio in the prior art.

Description

Technical Field

[0001] The invention relates to the technical field of chemical equipment, and in particular to a gas-liquid mixer and application thereof in cumene oxidation. Background Art

[0002] Multiphase reactions such as hydrogenation and oxidation are widely used in process industries, such as benzene hydrogenation, PX air oxidation, diesel fixed bed hydrogenation, etc. These reaction processes are severely restricted by heat transfer rate and mass transfer rate, which in turn affects the overall efficiency of the reaction. The fundamental reason is that the interphase area between gas and liquid and between gas, liquid and solid is too small. Taking the traditional bubbling air oxidation reactor as an example, since the bubble diameter is generally between 5-30mm, under normal pressure conditions, the interphase area between gas and liquid phases is usually 20-300m 2 ·m -3 , and in most cases less than 100m 2 ·m -3 Therefore, in industrial practice, people usually increase the gas circulation volume or add reactor internal components to enhance mass transfer and improve reaction, but the effect is very limited.

[0003] The principle of microinterface enhanced reaction technology (MIR) is to efficiently control the geometric scale of gas-liquid, gas-liquid-liquid, and gas-liquid-solid interfaces from milli-centimeter level to micrometer level, which greatly increases the interfacial area by an order of magnitude. When the bubble is gradually reduced from several millimeters to micrometer level, the gas-liquid mass transfer rate and reaction rate will be significantly enhanced, thereby doubling the efficiency of the chemical production process, significantly reducing energy consumption and material consumption, and improving safety and environmental protection performance. The key to microinterface enhanced reaction technology lies in the enhanced mixing between multiple phases, such as the enhanced mixing of gas and liquid phases. Therefore, the preparation of microbubbles is particularly important. The existing technology has gradually developed a preparation method for microbubbles suitable for different occasions. Specifically, according to the generation method of microbubbles, it is mainly divided into the following types: (1) shearing and breaking bubbles, such as Venturi type microbubble generator; (2) pressure reduction or temperature increase bubbles, such as pressure dissolution type microbubble generator; (3) ultrasonic bubble formation; (4) microporous bubble formation, such as microporous plastics, rubber and ceramic tubes.

[0004] In the existing technology, gas-liquid two-phase enhanced mixing technology is mainly used in water treatment, aquaculture, and medicine, and is less used in chemical production. The reason is that it is difficult to scale up the micromixer. One of the core issues is how to prepare microbubbles on a large scale and with high throughput. Another problem is that there are certain technical limitations in the preparation of microbubbles under high gas-liquid ratio conditions. Summary of the invention

[0005] The purpose of the present invention is to overcome the problem of poor gas-liquid two-phase mixing efficiency under high flux and high gas-liquid ratio conditions in the prior art, and to provide a gas-liquid mixer and its application in isopropylbenzene oxidation, which can effectively improve the mixing efficiency of the gas-liquid two-phase under high flux and high gas-liquid ratio conditions.

[0006] In order to achieve the above-mentioned objectives, the first aspect of the present invention provides a gas-liquid mixer, comprising a mixer shell having a first pressurized inflation zone and a second pressurized inflation zone, an injection pipe is arranged in the first pressurized inflation zone, and a porous material membrane tube is arranged in the second pressurized inflation zone, the injection pipe is coaxially connected with the porous material membrane tube to form a continuous internal flow channel for liquid to flow through; the injection pipe comprises a liquid inlet section, a throttling section, an air inlet section and a gas-liquid two-phase development section which are arranged in sequence along the flow direction of the liquid, the flow channel cross-sectional area of ​​the liquid inlet section is equal to that of the air inlet section and is larger than the flow channel cross-sectional area of ​​the throttling section, and the air inlet section and the porous material membrane tube are respectively used to introduce gas into the internal flow channel.

[0007] Preferably, a sieve plate is provided at the throttling section of the injection pipe, and a plurality of sieve holes are provided on the sieve plate.

[0008] Preferably, the sieve holes have a diameter of 1-3 mm, and the number of the sieve holes is 1-30, preferably 4-12.

[0009] Preferably, the angle between the axial direction of the sieve hole and the cross section of the injection pipe perpendicular to the length direction is 90°.

[0010] Preferably, the angle between the axial direction of the sieve hole and the cross section of the injection pipe perpendicular to the length direction is 30°-60°.

[0011] Preferably, one end of the air inlet section close to the throttling section is arranged to be spaced apart from the liquid outlet end of the throttling section.

[0012] Preferably, the distance between one end of the air inlet section close to the throttling section and the liquid outlet end of the throttling section is 1-10 mm, preferably 2-5 mm.

[0013] Preferably, the ratio of the length of the gas-liquid two-phase development section to the length of the air inlet section is 1-50:1, preferably 5-20:1.

[0014] Preferably, a plurality of the injection tubes are provided, and a plurality of the porous material membrane tubes are provided, and the plurality of the injection tubes are coaxially connected with the plurality of the porous material membrane tubes in a one-to-one correspondence to form a plurality of continuous internal flow channels for liquid to pass through.

[0015] Preferably, one end of the mixer shell is provided with an inlet head for connecting multiple injection tubes away from one end of the multiple porous material membrane tubes, and the other end of the mixer shell is provided with an outlet head for connecting multiple porous material membrane tubes away from one end of the multiple injection tubes.

[0016] The inlet cover is provided with a liquid inlet for liquid to enter, and the outlet cover is provided with an outlet for gas-liquid mixture to flow out.

[0017] Preferably, a liquid distributor connected to the liquid inlet is provided in the inlet head, and the liquid distributor is used to disperse the liquid into the internal flow channel.

[0018] Preferably, the outlet head is filled with filler.

[0019] Preferably, the tube wall of the injection tube located at the air inlet section is configured as a porous metal sintered film, and the average pore size of the metal sintered film is 1-50 μm, preferably 1-20 μm.

[0020] Preferably, the base material of the porous material membrane tube is selected from one of stainless steel, quartz, alumina, polytetrafluoroethylene, polypropylene and polyethylene.

[0021] Preferably, the pore size of the porous material membrane tube is 1-100 μm, preferably 3-10 μm.

[0022] Preferably, the porous material membrane tube is provided with a plurality of channels extending along its axial direction, and the plurality of channels are combined to form the internal flow channel for the liquid to flow through the porous material membrane tube.

[0023] Preferably, the number of the channels is 9-60, preferably 18-40.

[0024] Preferably, a porous structure coating is provided on the inner wall of each of the channels.

[0025] Preferably, the pore size of the porous structure coating is 20-800 nm, preferably 150-600 nm.

[0026] Preferably, an intermediate seal is provided between the first pressurized inflation zone and the second pressurized inflation zone.

[0027] The mixer housing is provided with a first air inlet for the gas to enter the first pressurized inflation zone and a second air inlet for the gas to enter the second pressurized inflation zone.

[0028] Preferably, a plurality of the first air inlet and a plurality of the second air inlet are respectively provided, and the plurality of the first air inlet and the plurality of the second air inlet are respectively arranged at intervals along the circumferential direction of the mixer housing.

[0029] The second aspect of the present invention provides an application of the aforementioned gas-liquid mixer in the oxidation of cumene, wherein the gas and liquid used for the cumene oxidation reaction are mixed in the gas-liquid mixer to form a gas-liquid mixture, and the gas-liquid mixture is transported to the cumene oxidation reactor through a pipeline for reaction; the gas is an oxygen-containing gas, and the liquid is a liquid containing cumene or an oxidation liquid containing cumene hydrogen peroxide.

[0030] Preferably, the internal flow channel located at the porous material membrane tube is loaded with catalyst active components; or

[0031] A filler is arranged at the outlet of the porous material membrane tube, and the filler is loaded with catalyst active components; or

[0032] A filler made of a material containing catalyst active components is arranged at the outlet of the porous material membrane tube.

[0033] Preferably, the catalyst active component is selected from at least one oxide of copper, magnesium, cobalt, manganese, nickel, chromium, zinc, iron, silver and gold.

[0034] Preferably, the loading amount of the catalyst active component is 0.01%-10% of the weight of the porous material membrane tube or the filler, preferably 0.05%-5%.

[0035] Preferably, the catalyst active components are loaded by impregnation, vacuum coating, chemical vapor deposition or atomic layer deposition.

[0036] Compared with the prior art, when the gas-liquid mixer provided by the present invention is used, the liquid enters from the end of the injection tube away from the porous material membrane tube, passes through the injection tube and the internal flow channel of the porous material membrane tube in turn, and pressurized gas is introduced into the first pressurized inflation zone and the second pressurized inflation zone. The pressurized gas enters the internal flow channel through the air inlet section and the porous material membrane tube, mixes with the liquid, and forms a gas-liquid mixture.

[0037] The present invention arranges two gas-liquid mixing areas in the flow direction of the liquid, and gas can be introduced into the internal flow channel in the two gas-liquid mixing areas, thereby ensuring the mixing efficiency of the gas-liquid two-phase under the conditions of high flux and high gas-liquid ratio; specifically, by arranging the injection pipe into a liquid inlet section, a throttling section, an air inlet section and a gas-liquid two-phase development section connected in sequence, in the process of the liquid entering the throttling section through the liquid inlet section, the flow rate of the liquid becomes faster due to the smaller cross-sectional area, and when entering the air inlet section, the pressure inside the liquid suddenly drops, causing the liquid to quickly diffuse to the surrounding area, generating violent eddy and turbulent phenomena, and this part of the liquid and the throttling section are mixed. The gas introduced through the air inlet section undergoes violent mixing friction to form a primary gas-liquid mixture rich in small bubbles. The gas and the liquid continue to interact and mix in the process of flowing through the gas-liquid two-phase development section, so that the mixing of the gas-liquid two-phases is more complete; further, the primary gas-liquid mixture rich in small bubbles enters the internal flow channel of the porous material membrane tube, and the pressurized gas in the second pressurized inflation zone enters the internal flow channel through the porous material membrane tube and is remixed with the primary gas-liquid mixture, which can not only effectively improve the gas-liquid ratio of the gas-liquid mixture, but also increase the bubble density in the gas-liquid mixture, thereby promoting the complete mixing of the gas-liquid two-phases.

[0038] The gas-liquid mixer provided by the present invention realizes efficient mixing of gas-liquid two-phases under high flux and high gas-liquid ratio conditions, effectively overcoming the defect of the prior art that a large number of micro-nano bubbles cannot be formed under high flux and high gas-liquid ratio conditions. BRIEF DESCRIPTION OF THE DRAWINGS

[0039] Figure 1 It is a structural schematic diagram of a gas-liquid mixer provided by the present invention;

[0040] Figure 2 This is a schematic diagram of a structure in which a single injection pipe and a porous material membrane tube are coaxially connected, provided by the present invention;

[0041] Figure 3 The diagram is a schematic diagram of the application of a gas-liquid mixer provided by the present invention in the oxidation of cumene.

[0042] Description of Reference Numerals

[0043] 1. Isopropylbenzene oxidation reactor; 10. Mixer shell; 101. First pressurized aeration zone; 102. Second pressurized aeration zone; 11. Inlet seal; 111. Liquid inlet; 12. Outlet seal; 121. Outlet; 13. Liquid distributor; 14. Packing; 15. Intermediate seal; 16. First air inlet; 17. Second air inlet; 20. Injection pipe; 21. Liquid inlet section; 22. Throttling section; 23. Air inlet section; 24. Gas-liquid two-phase development section; 25. Sieve plate; 251. Sieve hole; 30. Porous material membrane tube; 31. Channel. DETAILED DESCRIPTION

[0044] The specific implementation of the present invention is described in detail below in conjunction with the accompanying drawings. It should be understood that the specific implementation described here is only used to illustrate and explain the present invention, and is not used to limit the present invention.

[0045] As mentioned above, combined with Figure 1 , 2 As shown, the first aspect of the present invention provides a gas-liquid mixer for improving the mixing efficiency of gas and liquid under high flux and high gas-liquid ratio conditions.

[0046] The gas-liquid mixer includes a mixer shell 10 having a first pressurized inflation zone 101 and a second pressurized inflation zone 102, wherein an injection pipe 20 is arranged in the first pressurized inflation zone 101, and a porous material membrane tube 30 is arranged in the second pressurized inflation zone 102, wherein the injection pipe 20 is coaxially connected with the porous material membrane tube 30 to form a continuous internal flow channel for liquid to flow through; the injection pipe 20 includes a liquid inlet section 21, a throttling section 22, an air inlet section 23 and a gas-liquid two-phase development section 24 which are arranged in sequence along the flow direction of the liquid, the flow channel cross-sectional area of ​​the liquid inlet section 21 is equal to that of the air inlet section 23 and is larger than the flow channel cross-sectional area of ​​the throttling section 22, and the air inlet section 23 and the porous material membrane tube 30 are respectively used to introduce gas into the internal flow channel.

[0047] When the gas-liquid mixer provided by the present invention is used, the liquid enters from the end of the injection tube 20 away from the porous material membrane tube 30, passes through the internal flow channels of the injection tube 20 and the porous material membrane tube 30 in turn, and pressurized gas is introduced into the first pressurized inflation zone 101 and the second pressurized inflation zone 102. The pressurized gas enters the internal flow channel through the air inlet section 23 and the porous material membrane tube 30, mixes with the liquid, and forms a gas-liquid mixture.

[0048] The present invention sets two gas-liquid mixing areas in the flow direction of the liquid, and gas can be introduced into the internal flow channel in the two gas-liquid mixing areas, thereby ensuring the mixing efficiency of the gas-liquid two-phase under the conditions of high flux and high gas-liquid ratio; specifically, by setting the injection pipe 20 as a liquid inlet section 21, a throttling section 22, an air inlet section 23 and a gas-liquid two-phase development section 24 connected in sequence, in the process of the liquid entering the throttling section 22 through the liquid inlet section 21, the flow channel cross-sectional area becomes smaller and the flow rate of the liquid becomes faster. When entering the air inlet section 23, the pressure inside the liquid suddenly drops, causing the liquid to quickly diffuse to the surrounding area, generating violent vortex and turbulence phenomena. The liquid and the gas introduced through the air inlet section 23 undergo intense mixing friction to form a primary gas-liquid mixture rich in small bubbles. The gas and the liquid continue to interact and mix in the process of flowing through the gas-liquid two-phase development section 24, so that the mixing of the gas-liquid two-phases is more complete; further, the primary gas-liquid mixture rich in small bubbles enters the internal flow channel of the porous material membrane tube 30, and the pressurized gas in the second pressurized inflation zone 102 enters the internal flow channel through the porous material membrane tube 30 and is remixed with the primary gas-liquid mixture, which can not only effectively improve the gas-liquid ratio of the gas-liquid mixture, but also increase the bubble density in the gas-liquid mixture, thereby promoting the complete mixing of the gas-liquid two-phases.

[0049] In the gas-liquid mixer provided by the present invention, by setting two gas-liquid mixing zones and cooperating with the injection tube 20 and the porous material membrane tube 30 to gradually mix the gas-liquid two phases, efficient mixing of the gas-liquid two phases under high flux and high gas-liquid ratio conditions is achieved, effectively overcoming the defect of the prior art that a large number of micro-nano bubbles cannot be formed under high flux and high gas-liquid ratio conditions.

[0050] In the present invention, the injection pipe 20 is based on the Venturi principle, and uses the throttling section 22 to generate violent eddy and turbulent phenomena in the liquid, thereby achieving efficient mixing with the gas entering the internal flow channel from the air inlet section 23. In one embodiment of the present invention, a sieve plate 25 is provided at the throttling section 22 of the injection pipe 20, and a plurality of sieve holes 251 are provided on the sieve plate 25. By providing the sieve plate 25 with a plurality of sieve holes 251 on the flow path of the liquid, the liquid passing through the throttling section 22 is fully disturbed, thereby promoting efficient mixing between the liquid and the gas.

[0051] In the present invention, the aperture and number of the sieve holes 251 can be adaptively selected according to the specific type of the liquid, so that the liquid can generate sufficient eddy currents and turbulences in the air inlet section 23, thereby achieving efficient mixing of the liquid and the gas. In some embodiments of the present invention, the aperture of the sieve holes 251 is 1-3 mm, and the number of the sieve holes 251 is 1-30, preferably 4-12.

[0052] In some embodiments, the angle between the axial direction of the sieve hole 251 and the cross section of the injection pipe 20 perpendicular to the length direction is 90°; through this structural design, the liquid flowing through the liquid inlet section 21 directly enters the multiple sieve holes 251 of the sieve plate 25, and after being compressed and accelerated, enters the air inlet section 23 for release.

[0053] In some embodiments, the angle between the axial direction of the sieve hole 251 and the cross-section of the injection pipe 20 perpendicular to the length direction is 30°-60°; at this time, the liquid flowing through the liquid inlet section 21 changes direction when entering the sieve hole 251 of the sieve plate 25, further increasing the degree of turbulence of the liquid after flowing through the throttling section 22, thereby promoting a more complete mixing of the liquid and the gas entering the internal flow channel through the air inlet section 23.

[0054] In some embodiments, the end of the air inlet section 23 close to the throttling section 22 is set to be spaced from the liquid outlet end of the throttling section 22; after the compression and acceleration of the throttling section 22, the liquid generates violent eddy and turbulent phenomena when leaving the throttling section 22, and by setting the interval, a certain space is provided for the eddy and turbulent flow of the liquid. Preferably, the distance between the end of the air inlet section 23 close to the throttling section 22 and the liquid outlet end of the throttling section 22 is 1-10 mm, more preferably 2-5 mm.

[0055] In some embodiments, the ratio of the length of the gas-liquid two-phase development section 24 to the length of the gas inlet section 23 is 1-50:1, preferably 5-20:1.

[0056] In some embodiments, the injection tubes 20 are provided in plurality, and the porous material membrane tubes 30 are provided in plurality, and the plurality of injection tubes 20 are coaxially connected with the plurality of porous material membrane tubes 30 in a one-to-one correspondence to form a plurality of continuous internal flow channels for liquid to pass through. In the present invention, by providing a plurality of parallel internal flow channels for passing liquid, and cooperating with the injection tubes 20 and the porous material membrane tubes 30 to introduce air into the internal flow channels, the contact area between the gas and liquid phases is increased under the condition of ensuring high flux of gas and liquid, and sufficient mixing between the gas and liquid phases is promoted.

[0057] It is understandable that the number of the internal flow channels connected in parallel in the mixer housing 10 is designed according to the required liquid phase flux. In one embodiment of the present invention, the outer diameter of a single injection pipe 20 and a single porous material membrane tube 30 is 10-50 mm, preferably 20-30 mm; the liquid phase flux is 30-1000 L / h, preferably 60-300 L / h; the gas flux per unit length is 30-10000 L / h, preferably 60-5000 L / h; the gas-liquid volume ratio per unit length is 0.1-10m -1 , preferably 0.5-4m -1 .

[0058] In some embodiments, an inlet seal 11 is provided at one end of the mixer housing 10 for connecting one end of the plurality of injection tubes 20 away from the plurality of porous material membrane tubes 30, and an outlet seal 12 is provided at the other end of the mixer housing 10 for connecting one end of the plurality of porous material membrane tubes 30 away from the plurality of injection tubes 20; a liquid inlet 111 is provided on the inlet seal 11 for liquid to enter, and an outlet 121 is provided on the outlet seal 12 for gas-liquid mixture to flow out. When the gas-liquid mixer of this embodiment is in operation, the liquid enters the inlet seal 11 through the liquid inlet 111, and then enters the plurality of internal flow channels, fully contacts with the gas to form tiny bubbles, and the gas-liquid mixture rich in tiny bubbles then enters the outlet seal 12, and is discharged from the gas-liquid mixer through the outlet 121.

[0059] It should be noted that, in the present invention, the inlet seal 11 can be arranged at one end of the mixer housing 10 in any appropriate form, as long as the inlet seal 11 can be effectively isolated from the first pressurized inflation zone 101. For example, the inlet seal 11 and one end of the mixer housing 10 are sealed with a gasket, sealed with a metal mechanical seal, welded or glued, etc., preferably sealed with a metal mechanical seal or welded.

[0060] Similarly, the outlet seal 12 can be arranged at the other end of the mixer housing 10 in any appropriate form, as long as the outlet seal 12 can be effectively isolated from the second pressurized inflation zone 102. For example, the outlet seal 12 and the other end of the mixer housing 10 are sealed by gasket pressure, metal mechanical pressure, welding or gluing, preferably by gasket pressure.

[0061] In some embodiments, a liquid distributor 13 connected to the liquid inlet 111 is provided in the inlet seal 11, and the liquid distributor 13 is used to disperse the liquid into the internal flow channel. By providing the liquid distributor 13, it is ensured that the liquid can enter each internal flow channel evenly.

[0062] It is understandable that the liquid distributor 13 can be in any appropriate form, as long as it can evenly distribute the liquid entering the inlet head 11 to each internal flow channel. For example, the liquid distributor 13 is a branch-shaped porous row pipe, a ring-shaped porous row pipe, a trough distributor, a baffle distributor or a metal sintered distributor. Preferably, the liquid distributor 13 is a metal sintered distributor, a branch-shaped porous row pipe or a ring-shaped porous row pipe.

[0063] In some embodiments, the outlet seal 12 is filled with a filler 14. It should be noted that, in this embodiment, the gas-liquid mixture rich in tiny bubbles is already entering the outlet seal 12, and the filler 14 can further increase the turbulence of the gas-liquid mixture, achieve segmentation disturbance of the gas-liquid mixture, and promote the generation of more tiny bubbles.

[0064] It should be noted that the structure of the filler 14 can be in any appropriate form as long as it can promote the generation of more tiny bubbles. The shape of the filler 14 can be specifically selected as a ball ring, a Raschig ring, a corrugated mesh or a hollow sphere.

[0065] In addition, for some gas-liquid phase reactions that require a catalyst, by loading the corresponding catalyst in the filler 14, an efficient gas-liquid phase reaction can be simultaneously achieved at the end of the gas-liquid mixer; further, the filler 14 is directly prepared from a material containing a catalyst active component.

[0066] It is understandable that, in the present invention, the injection pipe 20 needs to meet the requirements of air-pressure differential strength. Considering the cost, the wall thickness of the injection pipe 20 is 1-5 mm, and more preferably 1-2 mm.

[0067] In the present invention, a portion of the gas in the gas-liquid mixture enters the internal flow channel through the air inlet section 23 of the injection pipe 20. In some embodiments, the tube wall of the injection pipe 20 located at the air inlet section 23 is set as a porous metal sintered film, and the average pore size of the metal sintered film is 1-50μm, preferably 1-20μm. Specifically, the metal material used to prepare the metal sintered film is titanium, carbon steel, stainless steel or Hastelloy, preferably stainless steel or Hastelloy.

[0068] Further, in the present invention, another part of the gas in the gas-liquid mixture enters the internal flow channel through the porous material membrane tube 30. In some embodiments, the base material of the porous material membrane tube 30 is selected from one of stainless steel, quartz, alumina, polytetrafluoroethylene, polypropylene, and polyethylene; preferably stainless steel or alumina. The wall of the porous material membrane tube 30 is a porous structure with a pore size of 1-100 μm, preferably 3-10 μm.

[0069] It can be understood that by preforming the base material used to prepare the porous material membrane tube 30 into a tube shape and cooperating with a sintering treatment, a porous material membrane tube 30 having an internal flow channel and a porous tube wall structure can be obtained. During specific use, the liquid flows in the internal flow channel, and the pressurized gas penetrates into the internal flow channel through the porous structure on the tube wall, mixes with the liquid, and forms a gas-liquid mixture.

[0070] In some embodiments, the porous material membrane tube 30 is provided with a plurality of channels 31 extending along its axial direction, and the plurality of channels 31 are combined to form the internal flow channel for the liquid to flow through the porous material membrane tube 30; by providing the plurality of channels 31, the contact area between the gas and the liquid is significantly increased, the aeration area is increased, and the gas flux and the gas-liquid ratio are improved.

[0071] In some embodiments, the number of the channels 31 is set to 9-60, preferably 18-40.

[0072] In some embodiments, a porous structure coating is provided on the inner wall of each of the channels 31; the pore size of the porous structure coating is 20-800nm, preferably 150-600nm. By providing a nano-scale porous structure coating in the channel 31, the gas penetrates into the internal flow channel through the porous structure coating, thereby generating more tiny bubbles. Specifically, the porous structure coating is formed by sintering a nano material, and the nano material is an oxide, preferably aluminum oxide, zirconium oxide, silicon dioxide or titanium dioxide.

[0073] In the present invention, an intermediate seal 15 is provided between the first pressurized gas zone 101 and the second pressurized gas zone 102, and a first air inlet 16 for the gas to enter the first pressurized gas zone 101 and a second air inlet 17 for the gas to enter the second pressurized gas zone 102 are provided on the mixer housing 10. The interior of the mixer housing 10 is separated by the intermediate seal 15 to form an independent first pressurized gas zone 101 and a second pressurized gas zone 102, so that the operation of introducing gas into the internal flow channel through the air inlet section 23 of the injection pipe 20 and the operation of introducing gas into the internal flow channel through the porous material membrane tube 30 do not affect each other.

[0074] It should be noted that, in the present invention, the intermediate seal 15 can be arranged in the mixer housing 10 in any appropriate form, as long as it can effectively isolate the first pressurized inflation zone 101 from the second pressurized inflation zone 102. For example, the intermediate seal 15 and the mixer housing 10 are sealed by gasket pressure, metal mechanical pressure, welding or gluing, etc., preferably gasket pressure sealing.

[0075] Furthermore, the first air inlet 16 and the second air inlet 17 are provided in plurality, and the plurality of the first air inlet 16 and the plurality of the second air inlet 17 are provided at intervals along the circumference of the mixer housing 10. By providing the plurality of first air inlets 16 and the plurality of second air inlets 17, the gas flux is increased, and the uniformity of the gas entering the internal flow channel through the air inlet section 23 and the porous material membrane tube 30 is also increased.

[0076] In some embodiments, the first air inlets 16 and the second air inlets 17 are respectively arranged in 1-5 groups, preferably 2-3 groups, and each group of the first air inlets 16 and each group of the second air inlets 17 are respectively symmetrically arranged along the center of the mixer housing 10 .

[0077] In the present invention, the length of the mixer shell 10 depends on the total length of the injection pipe 20 and the porous material membrane tube 30 and the number of parallel connections thereof. The diameter of the mixer shell 10 can be designed according to the heat exchanger shell design specification.

[0078] The gas-liquid mixer provided by the present invention is further described below through specific embodiments.

[0079] Example 1

[0080] This embodiment provides a Figure 1 The gas-liquid mixer shown in the figure comprises a mixer housing 10, an inlet head 11 arranged at one end of the mixer housing 10, and an outlet head 12 arranged at the other end of the mixer housing 10; the inlet head 11 and one end of the mixer housing 10 are sealed by gasket pressure; the outlet head 12 and the other end of the mixer housing 10 are sealed by gasket pressure. The inlet head 11 is provided with a liquid inlet 111 for liquid to enter, and a liquid distributor connected to the liquid inlet 111 is provided inside the inlet head 11, and the liquid distributor is a branch-type distributor; the outlet head 12 is provided with an outlet 121 for gas-liquid mixture to flow out, and the outlet head 12 is filled with Raschig ring packing.

[0081] The inner diameter of the mixer housing 10 is 80 mm;

[0082] A first pressurized aeration zone 101 having three injection tubes 20 and a second pressurized aeration zone 102 having three porous material membrane tubes 30 are arranged in the mixer housing 10; the three injection tubes 20 and the three porous material membrane tubes 30 are coaxially connected one by one to form three continuous internal flow channels for liquid to flow through.

[0083] The outer diameter of the injection tube 20 and the porous material membrane tube 30 is 30 mm;

[0084] The injection pipe 20 includes a liquid inlet section 21, a throttling section 22, a gas inlet section 23 and a gas-liquid two-phase development section 24 which are sequentially arranged along the flow direction of the liquid.

[0085] A sieve plate 25 is arranged in the injection pipe 20 at the throttling section 22. Eight sieve holes 251 are arranged on the sieve plate 25. The apertures of the eight sieve holes 251 are 1 mm respectively.

[0086] The angle between the axial direction of the sieve hole 251 and the cross section of the injection pipe 20 perpendicular to the length direction is 60°; the distance between the end of the air inlet section 23 close to the throttling section 22 and the liquid outlet end of the throttling section 22 is 1 mm.

[0087] The length of the gas-liquid two-phase development section 24 is 10 mm, and the length of the air intake section 23 is 1 mm.

[0088] The tube wall of the injection tube 20 located in the air inlet section 23 is a porous stainless steel sintered membrane with an average pore size of 10μm and a length of 1mm; the porous material membrane tube 30 is made of alumina and has a tube wall pore size of 5μm; the porous material membrane tube 30 is provided with 37 channels 31 extending axially, and a porous structure coating is provided on the inner wall of the channel 31. The material of the porous structure coating is nano-alumina with a pore size of 200nm.

[0089] The gas-liquid mixer provided in this embodiment is used to mix ethanol and air, wherein the feed flow rate of ethanol is 3 L / min, and the feed flow rate of air is 6 L / min.

[0090] The bubble imaging monitoring system was used to perform statistical analysis on the bubble sizes in the gas-liquid mixture flowing out of the outlet 121 , and the average bubble size was found to be 102 μm.

[0091] Example 2

[0092] The gas-liquid mixer provided in Example 1 was used to mix benzene and air, wherein the feed flow rate of benzene was 3 L / min and the feed flow rate of air was 6 L / min.

[0093] The bubble imaging monitoring system was used to perform statistical analysis on the bubble sizes in the gas-liquid mixture flowing out of the outlet 121 , and the average bubble size was found to be 164 μm.

[0094] Example 3

[0095] The gas-liquid mixer provided in Example 1 was used to mix water and air, wherein the feed flow rate of water was 3 L / min and the feed flow rate of air was 6 L / min.

[0096] The bubble imaging monitoring system was used to statistically analyze the bubble sizes in the gas-liquid mixture flowing out of the outlet 121 , and the average bubble size was found to be 281 μm.

[0097] Example 4

[0098] The gas-liquid mixer provided in Example 1 was used to mix ethanol and air, wherein the feed flow rate of ethanol was 3 L / min and the feed flow rate of air was 12 L / min.

[0099] The bubble imaging monitoring system was used to perform statistical analysis on the bubble sizes in the gas-liquid mixture flowing out of the outlet 121 , and the average bubble size was found to be 173 μm.

[0100] Example 5

[0101] The gas-liquid mixer provided in Example 1 was used to mix ethanol and air, wherein the feed flow rate of ethanol was 6 L / min and the feed flow rate of air was 6 L / min.

[0102] The bubble imaging monitoring system was used to perform statistical analysis on the bubble sizes in the gas-liquid mixture flowing out of the outlet 121 , and the average bubble size was found to be 87 μm.

[0103] Example 6

[0104] The gas-liquid mixer provided in Example 1 was used to mix ethanol and air, wherein the feed flow rate of ethanol was 12 L / min and the feed flow rate of air was 6 L / min.

[0105] The bubble imaging monitoring system was used to perform statistical analysis on the bubble sizes in the gas-liquid mixture flowing out of the outlet 121 , and the average bubble size was found to be 54 μm.

[0106] Example 7

[0107] The structure of the gas-liquid mixer provided in this embodiment is basically the same as that provided in embodiment 1, except that the inner diameter of the mixer housing 10 is 800 mm; the number of the injection pipes 20 and the porous material membrane pipes 30 is 30;

[0108] The gas-liquid mixer provided in this embodiment is used to mix ethanol and air, wherein the feed flow rate of ethanol is 300 L / min, and the feed flow rate of air is 600 L / min.

[0109] The bubble imaging monitoring system was used to perform statistical analysis on the bubble sizes in the gas-liquid mixture flowing out of the outlet 121 , and the average bubble size was found to be 108 μm.

[0110] Example 8

[0111] The structure of the gas-liquid mixer provided in this embodiment is basically the same as that provided in Embodiment 1, except that the aperture of the sieve hole 251 on the sieve plate 25 is 2 mm; the rest remains unchanged.

[0112] The gas-liquid mixer provided in this embodiment is used to mix ethanol and air, wherein the feed flow rate of ethanol is 3 L / min, and the feed flow rate of air is 6 L / min.

[0113] The bubble imaging monitoring system was used to perform statistical analysis on the bubble sizes in the gas-liquid mixture flowing out of the outlet 121 , and the average bubble size was found to be 131 μm.

[0114] Example 9

[0115] The structure of the gas-liquid mixer provided in this embodiment is basically the same as that provided in Embodiment 1, except that the length of the air inlet section 23 is 3 mm; the rest remains unchanged.

[0116] The gas-liquid mixer provided in this embodiment is used to mix ethanol and air, wherein the feed flow rate of ethanol is 3 L / min, and the feed flow rate of air is 6 L / min.

[0117] The bubble imaging monitoring system was used to perform statistical analysis on the bubble sizes in the gas-liquid mixture flowing out of the outlet 121 , and the average bubble size was found to be 166 μm.

[0118] Example 10

[0119] The structure of the gas-liquid mixer provided in this embodiment is basically the same as that in Embodiment 1, except that the distance between the end of the air inlet section 23 close to the throttling section 22 and the liquid outlet end of the throttling section 22 is 5 mm; the rest remains unchanged.

[0120] The gas-liquid mixer provided in this embodiment is used to mix ethanol and air, wherein the feed flow rate of ethanol is 3 L / min, and the feed flow rate of air is 6 L / min.

[0121] The bubble imaging monitoring system was used to perform statistical analysis on the bubble sizes in the gas-liquid mixture flowing out of the outlet 121 , and the average bubble size was found to be 234 μm.

[0122] Embodiment 11

[0123] The structures of the gas-liquid mixers provided in this embodiment are substantially the same as those provided in Embodiment 1, except that 10 channels 31 extending in the axial direction are provided on the porous material membrane tube 30; the rest remain unchanged.

[0124] The gas-liquid mixer provided in this embodiment is used to mix ethanol and air, wherein the feed flow rate of ethanol is 3 L / min, and the feed flow rate of air is 6 L / min.

[0125] The bubble imaging monitoring system was used to perform statistical analysis on the bubble sizes in the gas-liquid mixture flowing out of the outlet 121 , and the average bubble size was found to be 141 μm.

[0126] Example 12

[0127] The structure of the gas-liquid mixer provided in this embodiment is basically the same as that in Embodiment 1, except that the pore size of the porous structure coating in the channel 31 of the porous material membrane tube 30 is 1000 nm; the rest remains unchanged.

[0128] The gas-liquid mixer provided in this embodiment is used to mix ethanol and air, wherein the feed flow rate of ethanol is 3 L / min, and the feed flow rate of air is 6 L / min.

[0129] The bubble imaging monitoring system was used to perform statistical analysis on the bubble sizes in the gas-liquid mixture flowing out of the outlet 121 , and the average bubble size was found to be 223 μm.

[0130] Embodiment 13

[0131] The structure of the gas-liquid mixer provided in this embodiment is basically the same as that provided in Embodiment 1, except that the liquid distributor in the inlet header 11 is a baffle-type distributor; the rest remains unchanged.

[0132] The gas-liquid mixer provided in this embodiment is used to mix ethanol and air, wherein the feed flow rate of ethanol is 3 L / min, and the feed flow rate of air is 6 L / min.

[0133] The bubble imaging monitoring system was used to perform statistical analysis on the bubble sizes in the gas-liquid mixture flowing out of the outlet 121 , and the average bubble size was found to be 122 μm.

[0134] Embodiment 14

[0135] The structures of the gas-liquid mixers provided in this embodiment are basically the same as those provided in Embodiment 1, except that the liquid distributor in the inlet head 11 is a metal sintered distributor; the rest remain unchanged.

[0136] The gas-liquid mixer provided in this embodiment is used to mix ethanol and air, wherein the feed flow rate of ethanol is 3 L / min, and the feed flow rate of air is 6 L / min.

[0137] The bubble imaging monitoring system was used to perform statistical analysis on the bubble sizes in the gas-liquid mixture flowing out of the outlet 121 , and the average bubble size was found to be 89 μm.

[0138] Embodiment 15

[0139] The structure of the gas-liquid mixer provided in this embodiment is basically the same as that provided in Embodiment 1, except that the Raschig ring filler filled in the outlet head 12 is a corrugated mesh filler; the rest remains unchanged.

[0140] The gas-liquid mixer provided in this embodiment is used to mix ethanol and air, wherein the feed flow rate of ethanol is 3 L / min, and the feed flow rate of air is 6 L / min.

[0141] The bubble imaging monitoring system was used to statistically analyze the bubble sizes in the gas-liquid mixture flowing out of the outlet 121 , and the average bubble size was found to be 63 μm.

[0142] In the above test provided by the present invention, the smaller the average size of the bubbles obtained after the gas phase and the liquid phase are mixed, the better the effect of the gas-liquid two-phase mixing is.

[0143] Based on the above test data: The gas-liquid mixer provided by the present invention has a good gas-liquid mixing effect on different gas phases and liquid phases, and specifically can control the average size of the bubbles after gas-liquid mixing to be below 300μm. Combining the data of Examples 1, 4, 5, and 6, it can be seen that as the ratio of the gas feed amount to the liquid feed amount gradually decreases, the average size of the bubbles also gradually decreases; combining the data of Examples 1 and 7, it can be seen that the overall expansion of the specifications of the gas-liquid mixer of the present application has little effect on the average size of the bubbles; combining the data of Examples 1 and 8, it can be seen that increasing the aperture of the sieve hole 151 will lead to an increase in the average size of the bubbles; combining the data of Examples 1 and 9, it can be seen that increasing the length of the air intake section 23 is not conducive to reducing the average size of the bubbles; combining the data of Examples 1 and 10, it can be seen that increasing the distance between the end of the air intake section 23 close to the throttling section 22 and the throttling section The spacing between the liquid outlet ends of 22 is not conducive to reducing the average size of the bubbles; combined with the data of Examples 1 and 11, it can be seen that reducing the number of channels 31 will increase the average size of the bubbles; combined with the data of Examples 1 and 12, it can be seen that increasing the pore size of the porous structure coating in the channel 31 will increase the average size of the bubbles; combined with the data of Examples 1, 13, and 14, it can be seen that different liquid distributors will affect the average size of the bubbles, and the metal sintered distributor is the best; combined with the data of Examples 1 and 15, it can be seen that the corrugated mesh filler is better than the Raschig ring filler, and bubbles with relatively low average size can be obtained by using the corrugated mesh filler.

[0144] The gas-liquid mixer provided by the present invention is suitable for the mixing process of gas and liquid under high flux and high gas-liquid ratio conditions, and uses liquid to divide the gas to form micron-level tiny bubbles. The gas includes non-condensable gas and steam, the non-condensable gas includes oxygen, hydrogen, air, carbon monoxide and ammonia, etc., and the steam includes various organic or inorganic steam.

[0145] The gas-liquid mixer provided by the present invention can be applied to gas-liquid-solid three-phase or gas-liquid two-phase oxidation, hydrogenation, ammonia oxidation, nitration, chlorination, fluorination and other processes. In particular, the inventors of the present application found that the gas-liquid mixer provided by the present invention has a significant promoting effect in the cumene oxidation process.

[0146] Based on this, combined Figure 3As shown, the second aspect of the present invention provides an application of the aforementioned gas-liquid mixer in the oxidation of isopropylbenzene, wherein the gas and liquid used for the oxidation reaction of isopropylbenzene are mixed in the gas-liquid mixer to form a gas-liquid mixture, and the gas-liquid mixture is transported to the isopropylbenzene oxidation reactor 1 through a pipeline for reaction; the gas is an oxygen-containing gas, and the liquid is a liquid containing isopropylbenzene or an oxidation liquid containing isopropylbenzene hydrogen peroxide.

[0147] Cumene hydroperoxide, referred to as CHP, is an organic aromatic hydrocarbon derivative that can be used for arsenic removal from ethylene pyrolysis gasoline and the production of ABS graft polymerization initiators, epoxy compound oxidants, and phenol acetone. However, the traditional cumene oxidation process has many defects, such as slow reaction rate and low selectivity of the target product. In recent years, research on cumene oxidation process at home and abroad has mainly focused on improving conversion rate and selectivity. The reaction temperature and pressure are high, the cost is also high, and because the cumene oxidation reaction mechanism is relatively complex and is essentially a slow reaction process, the effect of improving process conditions is also very limited.

[0148] Although the use of catalysts can significantly improve the oxidation efficiency, it will make the process more complicated, and many problems in the separation and reuse of catalysts still exist; non-catalytic oxidation has been widely used in industrial applications, but its initial reaction speed is very slow, and there is a long induction period, which is not conducive to large-scale production. In order to overcome the above technical problems, industrial production uses low-content CHP as an initiator to accelerate the free radical chain reaction and achieve the purpose of shortening or eliminating the induction period. In addition, a small amount of organic acid is usually produced during the oxidation process, which causes CHP to decompose, thereby reducing the yield of CHP. In order to prevent side reactions (by-products such as 2-phenyl-2-propanol (PP) and acetophenone (AP)) and excessive decomposition of CHP, the conversion rate of isopropylbenzene is usually controlled to be less than 30%, but the problems of slow oxidation rate and large energy consumption of reaction equipment have not been significantly improved.

[0149] The inventors of the present application have discovered that by adopting the gas-liquid mixer provided by the present invention, the contact interface between the gas-liquid phases during the oxidation of cumene is effectively improved, and the micron-sized bubbles formed under high-flux, high-gas-liquid ratio conditions significantly increase the oxidation rate.

[0150] According to one embodiment of the present invention, the internal flow channel located at the porous material membrane tube 30 is loaded with catalytic active components; by coupling the catalytic active components in the porous material membrane tube 30, the catalyst separation problem in the oxidation of isopropylbenzene is effectively solved, and the micron-sized tiny bubbles generated in the porous material membrane tube 30 are combined to increase the contact area between gas-liquid-solid, thereby further improving the oxidation efficiency of isopropylbenzene and CHP selectivity.

[0151] According to another embodiment of the present invention, a filler 14 is provided at the outlet of the porous material membrane tube 30, and the filler 14 is loaded with catalyst active components; in this embodiment, the material of the filler 14 can be selected from alumina, titanium dioxide, cerium oxide, zirconium oxide or molecular sieve, preferably alumina, titanium dioxide and molecular sieve; the size of the filler 14 is 1-10 mm, preferably 2-5 mm. The catalyst active components are loaded on the filler 14 in any appropriate form, such as impregnation, vacuum coating, chemical vapor deposition or atomic layer deposition.

[0152] According to another embodiment of the present invention, a filler 14 made of a material containing catalyst active components is provided at the outlet of the porous material membrane tube 30. In this embodiment, the catalyst powder can be prepared by coprecipitation or deposition precipitation, and then further shaped to obtain the filler 14.

[0153] In the application of the gas-liquid mixer provided by the present invention in the oxidation of cumene, the structure of the filler 14 can be in any appropriate form, as long as it can conveniently load the catalyst and promote the generation of more tiny bubbles. The shape of the filler 14 can be specifically selected as a ball ring, a Raschig ring, a corrugated mesh or a hollow sphere, preferably a corrugated mesh or a hollow sphere.

[0154] In the present invention, by providing a filler 14 and further loading a catalyst active component on the filler 14, the filler 14 can further increase the turbulence of the gas-liquid mixture, achieve segmentation disturbance of the gas-liquid mixture, promote the generation of more tiny bubbles, and cooperate with the loaded catalyst active component to further improve the oxidation efficiency and selectivity of isopropylbenzene.

[0155] In the present invention, the catalyst active component is selected from at least one oxide of copper, magnesium, cobalt, manganese, nickel, chromium, zinc, iron, silver and gold; further, the loading amount of the catalyst active component is 0.01%-10% of the weight of the porous material membrane tube 30 or the filler 14, preferably 0.05%-5%; further, the catalyst active component is loaded by impregnation, vacuum coating, chemical vapor deposition or atomic layer deposition.

[0156] The application of the gas-liquid mixer provided by the present invention in the oxidation of cumene is further illustrated below through specific application examples.

[0157] Application Example 1

[0158] In this application example, the gas-liquid mixer provided in Example 1 is used to mix cumene hydroperoxide and air (oxygen concentration 21% (by volume percentage)) with a gas-liquid mixture, the gas feed rate is 6 L / min, and the liquid feed rate is 3 L / min; the obtained gas-liquid mixture is transported to the cumene oxidation reactor through a pipeline for reaction; the reaction temperature is maintained at 100° C., the reaction pressure is 0.3 MPaG, the initial concentration of cumene hydroperoxide is 14 wt %, and after 6 hours, the concentration of cumene hydroperoxide is analyzed by iodine titration, and other by-products, such as acetophenone and dimethylbenzyl alcohol, are analyzed by liquid chromatography; the reaction results are summarized in Table 1.

[0159] In the gas-liquid mixer, the porous material membrane tube 30 and the filler 14 are both loaded with CuO active components. The catalyst active components on the porous material membrane tube 30 are loaded in an amount of 1% of the mass of the porous material membrane tube 30, calculated as Cu; the catalyst active components on the filler 14 are loaded in an amount of 1% of the mass of the filler 14, calculated as Cu.

[0160] Application Example 2

[0161] This application example is basically the same as application example 1, except that the gas is replaced with oxygen-enriched gas (oxygen concentration is 50% (by volume percentage)); the other conditions remain unchanged, and the final analysis results are summarized in Table 1.

[0162] Application Example 3

[0163] This application example is basically the same as application example 1, except that the feed rate of the liquid is controlled to be 6 L / min, and the rest remains unchanged. The final analysis results are summarized in Table 1.

[0164] Application Example 4

[0165] This application example is basically the same as application example 1, except that the feed rate of the liquid is controlled to be 1.5 L / min, and the other conditions remain unchanged. The final analysis results are summarized in Table 1.

[0166] Application Example 5

[0167] This application example is basically the same as application example 1, except that the catalyst active components on the porous material membrane tube 30 are loaded in an amount of 3% of the mass of the porous material membrane tube 30, calculated as Cu; the catalyst active components on the filler 14 are loaded in an amount of 3% of the mass of the filler 14, calculated as Cu; the other conditions remain unchanged, and the final analysis results are summarized in Table 1.

[0168] Application Example 6

[0169] This application example is basically the same as application example 1, except that the porous material membrane tube 30 and the filler 14 are both loaded with MgO active components, the loading amount remains unchanged, and the other conditions remain unchanged. The final analysis results are summarized in Table 1.

[0170] Application Example 7

[0171] This application example is basically the same as application example 1, except that the porous material membrane tube 30 and the filler 14 are not loaded with catalyst active components, and the other conditions remain unchanged. The final analysis results are summarized in Table 1.

[0172] The conventional aeration method was used as a comparative example. The gas phase feed rate during aeration was 6 L / min. The reaction results are summarized in Table 1.

[0173] Table 1:

[0174]

[0175]

[0176] It can be seen from the data of Application Example 1 and the comparative example that the gas-liquid mixer provided by the present invention can increase the reaction rate and improve the selectivity of CHP. It can be seen from the data of Application Examples 1 and 2 that the oxygen-enriched condition can increase the reaction rate, but is not conducive to the selectivity of CHP; it can be seen from the data of Application Examples 1, 3, and 4 that the gas-liquid ratio is reduced, the mixing effect is good, the reaction rate can be increased, and the selectivity of CHP can be improved; the gas-liquid ratio is increased, the oxidation rate is reduced, and it is not conducive to the selectivity of CHP; it can be seen from the data of Application Examples 1 and 5 that increasing the loading amount of the active components of the catalyst can increase the reaction rate but is not conducive to the selectivity of CHP; it can be seen from the data of Application Examples 1 and 6 that the reaction rate when MgO is loaded is better than that when CuO is loaded, but the selectivity of CHP when CuO is loaded is better than that of MgO; it can be seen from the data of Application Examples 1 and 7 that the loaded catalyst can increase the reaction rate, but has an effect on the selectivity of CHP.

[0177] The preferred embodiments of the present invention are described in detail above with reference to the accompanying drawings, but the present invention is not limited thereto. Within the technical concept of the present invention, the technical solution of the present invention can be subjected to a variety of simple modifications. In order to avoid unnecessary repetition, the present invention will not further describe various possible combinations. However, these simple modifications and combinations should also be regarded as the contents disclosed by the present invention and belong to the protection scope of the present invention.

Claims

1. A gas-liquid mixer, characterized in that: The mixer comprises a housing (10) having a first pressurized aeration zone (101) and a second pressurized aeration zone (102), wherein the first pressurized aeration zone (101) is provided with an injection pipe (20), and the second pressurized aeration zone (102) is provided with a porous material membrane tube (30), wherein the injection pipe (20) is coaxially connected with the porous material membrane tube (30) to form a continuous internal flow channel for liquid to flow through; The injection tube (20) comprises a liquid inlet section (21), a throttling section (22), an air inlet section (23) and a gas-liquid two-phase development section (24) which are sequentially arranged along the flow direction of the liquid. The flow channel cross-sectional area of ​​the liquid inlet section (21) is equal to that of the air inlet section (23) and is larger than that of the throttling section (22). The air inlet section (23) and the porous material membrane tube (30) are respectively used to introduce gas into the internal flow channel.

2. The gas-liquid mixer according to claim 1, characterized in that: A sieve plate (25) is provided at the throttling section (22) of the injection pipe (20), and a plurality of sieve holes (251) are provided on the sieve plate (25); Preferably, the pore size of the sieve hole (251) is 1-3 mm, and the number of the sieve holes (251) is 1-30, preferably 4-12; Preferably, the angle between the axial direction of the sieve hole (251) and the cross section of the injection pipe (20) perpendicular to the length direction is 90°; Preferably, the angle between the axial direction of the sieve hole (251) and the cross section of the injection pipe (20) perpendicular to the length direction is 30°-60°.

3. The gas-liquid mixer according to claim 1, characterized in that: One end of the air inlet section (23) close to the throttling section (22) is arranged to be spaced apart from the liquid outlet end of the throttling section (22); Preferably, the distance between one end of the air inlet section (23) close to the throttling section (22) and the liquid outlet end of the throttling section (22) is 1-10 mm, preferably 2-5 mm.

4. The gas-liquid mixer according to claim 1, characterized in that: The ratio of the length of the gas-liquid two-phase development section (24) to the length of the air inlet section (23) is 1-50:1, preferably 5-20:

1.

5. The gas-liquid mixer according to claim 1, characterized in that: A plurality of injection tubes (20) are provided, and a plurality of porous material membrane tubes (30) are provided. The plurality of injection tubes (20) are coaxially connected with the plurality of porous material membrane tubes (30) in a one-to-one correspondence to form a plurality of continuous internal flow channels for liquid to pass through.

6. The gas-liquid mixer according to claim 5, characterized in that: One end of the mixer housing (10) is provided with an inlet seal (11) for connecting one end of the plurality of injection tubes (20) away from the plurality of porous material membrane tubes (30), and the other end of the mixer housing (10) is provided with an outlet seal (12) for connecting one end of the plurality of porous material membrane tubes (30) away from the plurality of injection tubes (20); The inlet seal (11) is provided with a liquid inlet (111) for liquid to enter, and the outlet seal (12) is provided with an outlet (121) for gas-liquid mixture to flow out.

7. The gas-liquid mixer according to claim 6, characterized in that: A liquid distributor (13) connected to the liquid inlet (111) is arranged inside the inlet seal (11), and the liquid distributor (13) is used to disperse the liquid into the internal flow channel.

8. The gas-liquid mixer according to claim 6, characterized in that: The outlet sealing head (12) is filled with a filler (14).

9. The gas-liquid mixer according to claim 1, characterized in that: The tube wall of the injection tube (20) located in the air inlet section (23) is configured as a porous metal sintered film, and the average pore size of the metal sintered film is 1-50 μm, preferably 1-20 μm.

10. The gas-liquid mixer according to claim 1, characterized in that: The base material of the porous material membrane tube (30) is selected from one of stainless steel, quartz, alumina, polytetrafluoroethylene, polypropylene and polyethylene; Preferably, the pore size of the porous material membrane tube (30) is 1-100 μm, preferably 3-10 μm.

11. The gas-liquid mixer according to claim 1, characterized in that: The porous material membrane tube (30) is provided with a plurality of channels (31) extending along its axial direction, and the plurality of channels (31) are combined to form the internal flow channel for the liquid to flow through the porous material membrane tube (30); Preferably, the number of the channels (31) is 9-60, preferably 18-40; Preferably, a porous structure coating is provided on the inner wall of each of the channels (31); Preferably, the pore size of the porous structure coating is 20-800 nm, preferably 150-600 nm.

12. The gas-liquid mixer according to claim 1, characterized in that: An intermediate sealing member (15) is provided between the first pressurized inflation zone (101) and the second pressurized inflation zone (102); The mixer housing (10) is provided with a first air inlet (16) for the gas to enter the first pressurized inflation zone (101) and a second air inlet (17) for the gas to enter the second pressurized inflation zone (102).

13. The gas-liquid mixer according to claim 12, characterized in that: A plurality of the first air inlet (16) and a plurality of the second air inlet (17) are provided, and the plurality of the first air inlet (16) and the plurality of the second air inlet (17) are arranged at intervals along the circumferential direction of the mixer housing (10).

14. Use of the gas-liquid mixer according to any one of claims 1 to 13 in cumene oxidation, characterized in that: The gas and liquid for cumene oxidation reaction are mixed in the gas-liquid mixer to form a gas-liquid mixture, and the gas-liquid mixture is transported to the cumene oxidation reactor (1) through a pipeline for reaction; The gas is an oxygen-containing gas, and the liquid is a liquid containing cumene or an oxidizing liquid containing cumene hydroperoxide.

15. Use of the gas-liquid mixer according to claim 14 in cumene oxidation, characterized in that: The internal flow channel located at the porous material membrane tube (30) is loaded with catalyst active components; or A filler (14) is provided at the outlet of the porous material membrane tube (30), and a catalyst active component is loaded on the filler (14); or A filler (14) made of a material containing catalyst active components is arranged at the outlet of the porous material membrane tube (30).

16. Use of the gas-liquid mixer according to claim 15 in cumene oxidation, characterized in that: The catalyst active component is selected from at least one oxide of copper, magnesium, cobalt, manganese, nickel, chromium, zinc, iron, silver and gold; Preferably, the loading amount of the catalyst active component is 0.01%-10% of the weight of the porous material membrane tube (30) or the filler (14), preferably 0.05%-5%; Preferably, the catalyst active components are loaded by impregnation, vacuum coating, chemical vapor deposition or atomic layer deposition.

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